CN103265056B - Method for extracting industrial slat from salt mixture - Google Patents
Method for extracting industrial slat from salt mixture Download PDFInfo
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- CN103265056B CN103265056B CN201310219204.XA CN201310219204A CN103265056B CN 103265056 B CN103265056 B CN 103265056B CN 201310219204 A CN201310219204 A CN 201310219204A CN 103265056 B CN103265056 B CN 103265056B
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- Prior art keywords
- salt
- dissolver
- particulate
- nacl
- solid
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- 238000000034 method Methods 0.000 title claims abstract description 26
- 239000011833 salt mixture Substances 0.000 title abstract 2
- 235000002639 sodium chloride Nutrition 0.000 claims abstract description 137
- 150000003839 salts Chemical class 0.000 claims abstract description 117
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 47
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 23
- 239000011780 sodium chloride Substances 0.000 claims abstract description 23
- 238000002156 mixing Methods 0.000 claims abstract description 15
- 239000007788 liquid Substances 0.000 claims abstract description 14
- 239000002699 waste material Substances 0.000 claims abstract description 6
- 239000005997 Calcium carbide Substances 0.000 claims abstract description 5
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 claims abstract description 5
- 238000001914 filtration Methods 0.000 claims abstract description 4
- 239000011541 reaction mixture Substances 0.000 claims abstract description 4
- 239000007790 solid phase Substances 0.000 claims abstract description 4
- 238000003756 stirring Methods 0.000 claims abstract description 4
- 238000007670 refining Methods 0.000 claims description 11
- 235000017550 sodium carbonate Nutrition 0.000 claims description 10
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical class O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 8
- 239000000243 solution Substances 0.000 claims description 7
- 230000002411 adverse Effects 0.000 claims description 6
- 230000009089 cytolysis Effects 0.000 claims description 6
- 238000002386 leaching Methods 0.000 claims description 6
- 239000002689 soil Substances 0.000 claims description 6
- 229910052749 magnesium Inorganic materials 0.000 claims description 5
- 239000011575 calcium Substances 0.000 claims description 4
- 229910019440 Mg(OH) Inorganic materials 0.000 claims description 3
- 229910052791 calcium Inorganic materials 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 abstract description 12
- 239000007787 solid Substances 0.000 abstract description 11
- 229910052943 magnesium sulfate Inorganic materials 0.000 abstract description 6
- 235000019341 magnesium sulphate Nutrition 0.000 abstract description 6
- 239000007791 liquid phase Substances 0.000 abstract description 5
- 239000012535 impurity Substances 0.000 abstract description 4
- 238000007599 discharging Methods 0.000 abstract 1
- 238000000227 grinding Methods 0.000 abstract 1
- 239000004576 sand Substances 0.000 abstract 1
- 239000011777 magnesium Substances 0.000 description 12
- 239000013078 crystal Substances 0.000 description 7
- 239000002994 raw material Substances 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 229910052938 sodium sulfate Inorganic materials 0.000 description 4
- 235000011152 sodium sulphate Nutrition 0.000 description 4
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910052804 chromium Inorganic materials 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000005096 rolling process Methods 0.000 description 2
- 229910021653 sulphate ion Inorganic materials 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229940037003 alum Drugs 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- ZCDOYSPFYFSLEW-UHFFFAOYSA-N chromate(2-) Chemical compound [O-][Cr]([O-])(=O)=O ZCDOYSPFYFSLEW-UHFFFAOYSA-N 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- LRIXWBJFBQKGBX-UHFFFAOYSA-J magnesium disodium disulfate tetrahydrate Chemical compound O.O.O.O.[Na+].[Na+].[Mg++].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O LRIXWBJFBQKGBX-UHFFFAOYSA-J 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 239000002362 mulch Substances 0.000 description 1
- 239000004800 polyvinyl chloride Substances 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a method for extracting industrial slat from salt mixture. The method comprises the following steps: grinding crude salt into fine salt through a crushing step, conveying the fine salt to a salt dissolver to rotate along with the salt dissolver, wherein the fine salt is pushed to the outlet through the stirring of blades arranged in spiral at the inner wall; filtering the fine salt treated by the salt dissolver, wherein the product can be directly used by the salt enterprise; enabling the liquid part in the salt dissolver with fine sand to flow into a blending pot to mixing and reacting with soda waste liquor and calcium carbide mud, removing the SO4<2-> and Mg<2+>, placing the reaction mixture into a settling tank to separate the solid from the liquor, filter-pressing the solid phase part, and discharging, flowing back a part of the clarified liquor into the salt dissolver to dissolve new fine salt, forming the circulation, wherein the other part of the clarified liquor is placed in a salt dissolving barrel to saturate the NaCl so as to be used for soda. The pure impurities containing SO42- such as solid NaCl, MgSO4 and the like are remained in the liquid phase, and the aims of separating and purifying are achieved.
Description
Technical field
The invention belongs to a kind of prepare Industrial Salt in mixing salt method, especially, in soda industry, utilize soda ash by product evaporated waste ammonia liquid to purify and separated mixing salt, obtain refining industrial salt.
Background technology
The crystal salt lid that the bloedite ore deposit Surface mulch of Ejina Banner has one deck 20～50 ㎝ not wait, this crystal salt lid is hereinafter to be referred as volume salt, and the main component of volume salt is NaCl, and NaCl content is 90～95%, and all the other are magnesium sulfate, Na
2sO
4, Ca
2+and insolubles, because of cannot crystal salt lid is thoroughly separated with vanthoffite layer in recovery process, inevitably to mix part vanthoffite, cause salt alum to mix, the NaCl content of this mixture is 60～90%, vanthoffite between 10～30%, concrete SO
2- 4content 10～20%, Mg
2+content 1～3%, as do industrial salt, its SO
2- 4, Mg
2+too high levels can not directly be used, and two kinds of compositions need be given to separation, and purification NaCl is convenient to directly be used by soda ash and chlor-alkali.
Chinese invention patent publication number is in the specification sheets of CN1058240, to disclose the separation method of a kind of vitriol of Canadian Chemetics International Co. Ltd, the method is from the aqueous solution of the chromium component containing contaminative, by the crystallization of sulphate cpd, isolate the method for vitriol, it specifically discloses following technical characterictic: " regulate the pH value of described solution in 2.0 to 6.5 scope, cooling this solution makes sulphate cpd from Precipitation wherein subsequently, remove subsequently the vitriol of Precipitation, the separable like this vitriol that goes out not basically contain chromium component.The method is extracted vitriol in being rich in the chromate waste water of sulfate radical, has increased the comprehensive utilization of waste water." but the method processing power is more single, aspect separated polycomponent blended solid salt, also has a lot of deficiencies.
Summary of the invention
The deficiency that the present invention exists in order to overcome prior art, a kind of method that provides mixing salt to obtain through refining Industrial Salt, this method can access purer solid NaCl, MgSO
4, SO
4 2-stayed in liquid phase, thereby reached object separated and that purify.
The present invention is achieved by the following technical solutions: a kind of mixing salt is obtained through refining the method for Industrial Salt, and it comprises the steps:
First a, crude salt grind to form through broken step the salt particulate that diameter is less than 5 millimeters, salt particulate is sieved, through tape transport to crude salt storage hopper;
Salt particulate in b, crude salt storage hopper again through tape transport to salt dissolver, the nearly saturated brine contact lysis that adverse current is come in salt particulate and desalinization of soil by flooding or leaching bucket, salt particulate follows salt dissolver to rotate, and is arranged in spiral blade stirs and push to outlet by inwall;
C, the salt particulate processed through salt dissolver filter through band filter, and the product finally obtaining is stacked by tape transport to saltern, for salt unit directly;
Nearly saturated brine is the gap between suitable salt dissolver intra vane in salt dissolver, with the crude salt particulate contact flow of rolling, gradually by the SO in crude salt particulate
4 2-and Mg
2+dissolve efflux of solids SO wherein when exporting
4 2-and Mg
2+the qualified solid salt of the basic complete one-tenth of separated and dissolved;
Liquid portion in d, salt dissolver carries thin silt particle and flows into convert and close in pot, reacts with waste soda ash solution and calcium carbide mud mix and blend, removes SO wherein
4 2-and Mg
2+, generate CaSO
4and Mg(OH)
2;
The reaction mixture of e, process d step process enters settling tank and carries out solid-liquid separation, and solid phase part is drained after press filtration;
In the clear liquor of f, solid-liquid separation, a part is got back in salt dissolver and is dissolved new salt particulate, forms circulation, and the another part in clear liquor makes NaCl saturated for soda ash through salt dissolving tank.
In b step, the nearly saturated brine that adverse current is come in salt particulate and desalinization of soil by flooding or leaching bucket is contact lysis under the condition of 35 ℃～45 ℃ in temperature, in dissolved salt particulate, contains SO
4 2-impurity.
The product index obtaining in c step is: NaCl content>=95%, SO
4 2-content≤0.5%, Ca
2+content≤0.2%, Mg
2+content≤0.09%
The principle that mixing salt of the present invention is obtained through refining Industrial Salt is: NaCl, magnesium sulfate and sodium sulfate can form a full curve altogether in the aqueous solution at a certain temperature, and its liquid phase forms constant.Because it is a large amount of that raw material forms NaCl content, thereby when the raw material of specified rate adds appropriate water and goes to dissolve, make magnesium sulfate in raw material, sodium sulfate just in common saturation point, dissolved complete, at this moment NaCl is also in saturation point, remaining NaCl solid and liquid equilibrium, no longer continue to dissolve in liquid phase, after solid-liquid separation, can obtain purer solid NaCl, MgSO
4deng containing SO
4 2-impurity stayed in liquid phase, thereby reached object separated and that purify.For obtaining as far as possible solid salt, molten can be with nearly saturated NaCl salt solution as solvent while soaking raw material, the mother liquor having dissolved after the magnesium nitre in raw material is processed for soda ash again, in raw material, salt can all be utilized like this.
The invention has the beneficial effects as follows: the technical problem to be solved in the present invention is in mixing salt, utilize NaCl and magnesium sulfate, sodium sulfate can not produce the complex salt crystal containing NaCl at crystallisation process, be magnesium sulfate, sodium sulfate can form vanthoffite complex salt crystal, the crystal of NaCl is single crystal, and vanthoffite is mechanically mixed in together, and the main component of mineral is NaCl, this just can utilize this characteristic that the NaCl in mixture is purified, and reaches separated SO from salt
2- 4, Mg
2+object.The present invention is the method for utilizing soda ash evaporated waste ammonia liquid, polyvinyl chloride by product calcium carbide mud to obtain through refining Industrial Salt in mixing salt, has advantages of economy, energy-saving and environmental protection.
Accompanying drawing explanation
Fig. 1 is that a kind of mixing salt of the present invention is obtained through refining the process flow sheet of the method for Industrial Salt.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described in detail.
As shown in Figure 1, a kind of mixing salt is obtained through refining the method for Industrial Salt, and it comprises the steps:
First a, crude salt grind to form through broken step the salt particulate that diameter is less than 5 millimeters, salt particulate is sieved, through tape transport to crude salt storage hopper;
Salt particulate in b, crude salt storage hopper again through tape transport to salt dissolver, the nearly saturated brine contact lysis that adverse current is come in salt particulate and desalinization of soil by flooding or leaching bucket, salt particulate follows salt dissolver to rotate, and is arranged in spiral blade stirs and push to outlet by inwall;
C, the salt particulate processed through salt dissolver filter through band filter, and the product finally obtaining is stacked by tape transport to saltern, for salt unit directly;
Nearly saturated brine is the gap between suitable salt dissolver intra vane in salt dissolver, with the crude salt particulate contact flow of rolling, gradually by the SO in crude salt particulate
4 2-and Mg
2+dissolve efflux of solids SO wherein when exporting
4 2-and Mg
2+the qualified solid salt of the basic complete one-tenth of separated and dissolved;
Liquid portion in d, salt dissolver carries thin silt particle and flows into convert and close in pot, reacts with waste soda ash solution and calcium carbide mud mix and blend, removes SO wherein
4 2-and Mg
2+, generate CaSO
4and Mg(OH)
2;
The reaction mixture of e, process d step process enters settling tank and carries out solid-liquid separation, and solid phase part is drained after press filtration;
In the clear liquor of f, solid-liquid separation, a part is got back in salt dissolver and is dissolved new salt particulate, forms circulation, and the another part in clear liquor makes NaCl saturated for soda ash through salt dissolving tank.
In b step, the nearly saturated brine that adverse current is come in salt particulate and desalinization of soil by flooding or leaching bucket is contact lysis under the condition of 35 ℃～45 ℃ in temperature, in dissolved salt particulate, contains SO
4 2-impurity.
The product index obtaining in c step is: NaCl content>=95%, SO
4 2-content≤0.5%, Ca
2+content≤0.2%, Mg
2+content≤0.09%
Finally should be noted that; above content is only in order to illustrate technical scheme of the present invention; but not limiting the scope of the invention; the simple modification that those of ordinary skill in the art carries out technical scheme of the present invention or be equal to replacement, does not all depart from essence and the scope of technical solution of the present invention.
Claims (2)
1. mixing salt is obtained through refining a method for Industrial Salt, it is characterized in that: the method that described mixing salt is obtained through refining Industrial Salt comprises the steps:
First a, crude salt grind to form through broken step the salt particulate that diameter is less than 5 millimeters, salt particulate is sieved, through tape transport to crude salt storage hopper;
Salt particulate in b, crude salt storage hopper again through tape transport to salt dissolver, the nearly saturated brine contact lysis that adverse current is come in salt particulate and desalinization of soil by flooding or leaching bucket, salt particulate follows salt dissolver to rotate, and is arranged in spiral blade stirs and push to outlet by inwall;
C, the salt particulate processed through salt dissolver filter through band filter, and the product finally obtaining is stacked by tape transport to saltern, for salt unit directly;
Liquid portion in d, salt dissolver carries thin silt particle and flows into convert and close in pot, reacts with waste soda ash solution and calcium carbide mud mix and blend, removes SO wherein
4 2-and Mg
2+, generate CaSO
4and Mg(OH)
2;
The reaction mixture of e, process d step process enters settling tank and carries out solid-liquid separation, and solid phase part is drained after press filtration;
In the clear liquor of f, solid-liquid separation, a part is got back in salt dissolver and is dissolved new salt particulate, forms circulation, and the another part in clear liquor makes NaCl saturated for soda ash through salt dissolving tank;
In described b step, the nearly saturated brine that adverse current is come in salt particulate and desalinization of soil by flooding or leaching bucket is contact lysis under the condition of 35 ℃～45 ℃ in temperature.
2. the method that a kind of mixing salt according to claim 1 is obtained through refining Industrial Salt, is characterized in that: the product index obtaining in described c step is: NaCl content>=92%, SO
4 2-content≤0.5%, Ca
2+content≤0.2%, Mg
2+content≤0.09%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310219204.XA CN103265056B (en) | 2013-06-05 | 2013-06-05 | Method for extracting industrial slat from salt mixture |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310219204.XA CN103265056B (en) | 2013-06-05 | 2013-06-05 | Method for extracting industrial slat from salt mixture |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103265056A CN103265056A (en) | 2013-08-28 |
| CN103265056B true CN103265056B (en) | 2014-11-19 |
Family
ID=49008736
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310219204.XA Active CN103265056B (en) | 2013-06-05 | 2013-06-05 | Method for extracting industrial slat from salt mixture |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103265056B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105502437A (en) * | 2015-11-26 | 2016-04-20 | 山东潍坊润丰化工股份有限公司 | Resourceful treatment technology of by-product industrial salt |
| CN108211413B (en) * | 2017-12-27 | 2020-07-21 | 地矿集团格尔木盐湖资源开发有限公司 | Solid-liquid separation and heaping-emptying technical method for purifying mineral salt blocks |
| CN109534361B (en) * | 2018-12-19 | 2021-03-09 | 青海盐湖工业股份有限公司 | Method for purifying sodium chloride from byproduct mixed salt |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1173466A (en) * | 1996-08-08 | 1998-02-18 | 天津长芦汉沽盐场有限责任公司 | Refined sodium chloride containing low calcium and magnesium and its prepn. method |
| CN202465305U (en) * | 2012-01-19 | 2012-10-03 | 江苏理文化工有限公司 | Salt leaching machine for reducing calcium magnesium salt mud content in crude salt for caustic soda device |
-
2013
- 2013-06-05 CN CN201310219204.XA patent/CN103265056B/en active Active
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| CN103265056A (en) | 2013-08-28 |
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Owner name: INNER MONGOLIA WUHAI CHEMICAL INDUSTRY LTD. Free format text: FORMER NAME: INNER MONGOLIA WUHAI CHEMICAL INDUSTRY CO., LTD. |
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| CP01 | Change in the name or title of a patent holder |
Address after: Haihua Industrial Park Hainan district the Inner Mongolia Autonomous Region City, Wuhai 016000 Patentee after: Inner Mongolia Wuhai Chemical Industry Ltd. Address before: Haihua Industrial Park Hainan district the Inner Mongolia Autonomous Region City, Wuhai 016000 Patentee before: Inner Mongolia Wuhai Chemical Industry Co., Ltd. |